CA2102160A1 - Remediation of low level radioactive mixed waste in a fluidized bed incinerator - Google Patents
Remediation of low level radioactive mixed waste in a fluidized bed incineratorInfo
- Publication number
- CA2102160A1 CA2102160A1 CA002102160A CA2102160A CA2102160A1 CA 2102160 A1 CA2102160 A1 CA 2102160A1 CA 002102160 A CA002102160 A CA 002102160A CA 2102160 A CA2102160 A CA 2102160A CA 2102160 A1 CA2102160 A1 CA 2102160A1
- Authority
- CA
- Canada
- Prior art keywords
- separator
- flue gas
- waste
- fluidized bed
- particles
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2203/00—Furnace arrangements
- F23G2203/50—Fluidised bed furnace
- F23G2203/501—Fluidised bed furnace with external recirculation of entrained bed material
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/18—Radioactive materials
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2217/00—Intercepting solids
- F23J2217/10—Intercepting solids by filters
- F23J2217/103—Intercepting solids by filters ultrafine [HEPA]
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S588/00—Hazardous or toxic waste destruction or containment
- Y10S588/90—Apparatus
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
Mixed waste containing organic constituents and low level radioactive waste is remediated in a circulating fluidized bed combustor. Three separators are used to filter the flue gas and separate fine radioactive material from coarse non-radioactive material thereby concentrating the radioactive portion.
A primary separator separates large material such as sand, lime, flyash or unburned fuel particles from the flue gas leaving the furnace of the combustor. The flue gas is then passed to a secondary separator for the collection of finer particles. In turn, the flue gas is passed to a tertiary separator for the collection of the finest particles of the flue gas containing low level radioactive waste. Solids entrained in the primary separator are recycled back into the bed of the combustor through an L-valve. Solids entrained at the secondary separator are also recycled back into the bed.
Mixed waste containing organic constituents and low level radioactive waste is remediated in a circulating fluidized bed combustor. Three separators are used to filter the flue gas and separate fine radioactive material from coarse non-radioactive material thereby concentrating the radioactive portion.
A primary separator separates large material such as sand, lime, flyash or unburned fuel particles from the flue gas leaving the furnace of the combustor. The flue gas is then passed to a secondary separator for the collection of finer particles. In turn, the flue gas is passed to a tertiary separator for the collection of the finest particles of the flue gas containing low level radioactive waste. Solids entrained in the primary separator are recycled back into the bed of the combustor through an L-valve. Solids entrained at the secondary separator are also recycled back into the bed.
Description
`:
!~ ' RE:MEDIATION OF LOW ~EVEL RADIOACTIVE MI~ED g~ASTE IN A
FLUIDIZED BED INCINERATOR
'' ~ BACKGROU~D OF TffE DNVENTION
: 1. Fieldofthe~nvention - The present invention relates in general to the ;~. 5 clean up of hazardous waste sites and in particular to a new and useful method and system for the remediation of low level radioactive mixed wastes in fluidized bed incinerators.
!~ ' RE:MEDIATION OF LOW ~EVEL RADIOACTIVE MI~ED g~ASTE IN A
FLUIDIZED BED INCINERATOR
'' ~ BACKGROU~D OF TffE DNVENTION
: 1. Fieldofthe~nvention - The present invention relates in general to the ;~. 5 clean up of hazardous waste sites and in particular to a new and useful method and system for the remediation of low level radioactive mixed wastes in fluidized bed incinerators.
2. DeQcription of the Related Ar : 10Improved disposal and treatment methods are required to clean up hazardous waste sites that have ~:', resulted from years of uncontrolled dumping. The preferred approach for disposal of the wastes is through a process that not only destroys the hazardous organic portion of the waste, but also separates the radioactive portion from the nonradioactive portion.
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2 Case 5279 Sl~ARY OF THE ~NVENTION
The present invention comprises the use of a circulating fluidized bed combustor to remediate mixed waste containing organic constituents and low level radioac~ive waste. The process capitalizes on three principles. First, since the low level radioactive waste is present primarily in very fine material, the natural size classification process of a circulating fluidized bed can be used to separate fine radioactive material from coarse non-radioactive material, thus concentrating the radioactive portion. Second, since the attrition, e.g., size breakdown of soil particles, in a circulating fluidized bed is high, even more fine material is generated, further concentrating the radioactive portion of the waste stream. Third, the circulating fluidized bed can be operated with a gas residence time of 1-2 seconds at 1700-1800F to destroy ; organic constituents in the waste such as dioxins, furans and PCBs.
20The various features of novelty which characterize the invention are pointed out with particularity in the claims annexed to and forming a ~! part of this disclosure. For a better understanding of the invention, its operating advantages and specific ``25 objects attained by its uses, reference is made to the iaccompanying drawings and descriptive matter in which the preferred embodiments of the invention are illustrated.
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2 Case 5279 Sl~ARY OF THE ~NVENTION
The present invention comprises the use of a circulating fluidized bed combustor to remediate mixed waste containing organic constituents and low level radioac~ive waste. The process capitalizes on three principles. First, since the low level radioactive waste is present primarily in very fine material, the natural size classification process of a circulating fluidized bed can be used to separate fine radioactive material from coarse non-radioactive material, thus concentrating the radioactive portion. Second, since the attrition, e.g., size breakdown of soil particles, in a circulating fluidized bed is high, even more fine material is generated, further concentrating the radioactive portion of the waste stream. Third, the circulating fluidized bed can be operated with a gas residence time of 1-2 seconds at 1700-1800F to destroy ; organic constituents in the waste such as dioxins, furans and PCBs.
20The various features of novelty which characterize the invention are pointed out with particularity in the claims annexed to and forming a ~! part of this disclosure. For a better understanding of the invention, its operating advantages and specific ``25 objects attained by its uses, reference is made to the iaccompanying drawings and descriptive matter in which the preferred embodiments of the invention are illustrated.
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3 Case 5279 BRIEF DESCRIPTION OF THE DRAWnNGS
In the drawings:
Fig. 1 is a side elevational view of a circulating fluidized bed combustor according the present invention; and Fig. 2 is a schematic drawing of a data acquisition system according to the present invention.
DESCRnPTION OF THE PREFERRED EMBOD~ENTS
Referring to the present invention embodied in Fig. 1, a circulating fluidized bed combustor system, generally designated 10 comprises a furnace 54 containing a bed of solid particles 50. Furnace 59 may be either a refractory lined incinerator or membrane - wall construction. The circulating fluidized bed combustor 10 has a fuel feeder 5 and sorbent feeder 7 positioned above the bed 50 for feeding the waste and sorbent into ~he bed 50. The combustor 10 can burn a variety of fuels such as waste coal, refuse derived fuel, tires, sludges, pulp, paper and wood waste. The combustor system 10 can also handle a~,widé/range of fuel~
feed sizes~ esmpar~-t~-~t~er--~n~inerators e.g.--rotary~
ki~, f~-r-e,;amp~, a- C~B~ ee~-normall-y-has-a-~ h~
~ize of-~b~ut 1 1~ ~hcs. ~ot~r-y kilns_can_feed 55 gallon drum~_ ~hus reducing the need for preprocessing~ /
the waste fuels. Feed from the sorbent feeder 7 and the f- ~ S
waste feeder 5 is provided to the bed 50 by means 9 for~
! feed transport. A burner 14 i5 provided at the furnace 54 for starting up the unit on an auxiliary fuel such as natural gas, prior to the introduction of mixed wastes 1~- L V :-J 1 ~ ~
'~
In the drawings:
Fig. 1 is a side elevational view of a circulating fluidized bed combustor according the present invention; and Fig. 2 is a schematic drawing of a data acquisition system according to the present invention.
DESCRnPTION OF THE PREFERRED EMBOD~ENTS
Referring to the present invention embodied in Fig. 1, a circulating fluidized bed combustor system, generally designated 10 comprises a furnace 54 containing a bed of solid particles 50. Furnace 59 may be either a refractory lined incinerator or membrane - wall construction. The circulating fluidized bed combustor 10 has a fuel feeder 5 and sorbent feeder 7 positioned above the bed 50 for feeding the waste and sorbent into ~he bed 50. The combustor 10 can burn a variety of fuels such as waste coal, refuse derived fuel, tires, sludges, pulp, paper and wood waste. The combustor system 10 can also handle a~,widé/range of fuel~
feed sizes~ esmpar~-t~-~t~er--~n~inerators e.g.--rotary~
ki~, f~-r-e,;amp~, a- C~B~ ee~-normall-y-has-a-~ h~
~ize of-~b~ut 1 1~ ~hcs. ~ot~r-y kilns_can_feed 55 gallon drum~_ ~hus reducing the need for preprocessing~ /
the waste fuels. Feed from the sorbent feeder 7 and the f- ~ S
waste feeder 5 is provided to the bed 50 by means 9 for~
! feed transport. A burner 14 i5 provided at the furnace 54 for starting up the unit on an auxiliary fuel such as natural gas, prior to the introduction of mixed wastes 1~- L V :-J 1 ~ ~
'~
4 Case 5279 ~ to the furnace. This provides heat to sustain the bed - temperature. Air lines 16 provide~ air to the furnace~ 9~ /
54. A wind box burner 12 preheats the air from the air~
lines 16.
~ater is provided in furnace cooling tubes 56 arranged through the furnace 54 to allow adjustment of bed temperatures.
Upon burning of materials within the bed 50, combustion gases emanate from the bed 50 and pass through the furnace 54 to a primary separator 20. The ~, primary separator 20 is located above the bed 50 and at the top of the furnace 54. The primary separator 20 is constructed of U-beams which are stainless steel channels installed in a labyrinth arrangement. The primary separator 20 removes large entrained bed material such as sand, lime, flyash or unburned fuel particles from the flue gas.
~` After passing through the primary separator 20, the combustion gas is then channeled through a convection pass cooling bundle 26 to a secondary cyclone .
separator 30. The secondary cyclone separator 30 separates fines from the flue gas.
After passing through the secondary cyclone separator 30 the flue gas is channeled through a second pass 36 to a tertiary separator 40 for tertiary separation~ The tertiary separator 40 may consist of a high efficiency particulate filter, such as a Hepa~
filter. Any solids collected at the tertiary separator 40 are channelled to a collection container 44.
~02~
~ 5 Case 5279 ,.~
Solids separated from the gas by the secondary cyclone separator 30 are recycled back into the bed 50 by a transport system 32 which recycles the solids to a recycle point 80 located near the furnace 54. The recycle point 80 then channels the recycled solids from the secondary cyclone separator 30 back into the bed 50.
Larger size solid particles captured by the primary separator 20 are channeled through a stand pipe 24 which runs parallel with the furnace 54 to a L-valve 22. The L-valve 22 transports these recycled solids directly into the bed 50. Additionally, solids can be discharged into a secondary collection container 34 located at the secondary cyclone separator 30.
Solids can be drained from the circulating fluidized bed combustor 10 by a bed drain 58 which directly drains solids from the bed 50, from the secondary cyclone 30 at the collection container 34 or ~ from the tertiary separator 40.
- Fig. 2 shows a computerized data acquisition 2Q system 90 for the continuous monitoring of operating conditions of the circulating fluidized bed combustor dat~ CrC ~ 5;h'orJ '~v,St~
10. The ~e~ 90 'periodically scans system~ ~ P~
temperatures, air and gas flow rates, and system static~
and differential pressures.
The flue gas exiting the tertiary collector 40 is continuously monitored for 2~ C unburned hydrocarbons and other gas constituents necessary to control the process. Thermocouple inputs 97 located at the circulating fluidized bed combustor 10 provide temperature information to the thermocouple junction 98 fJ.JL~?J ~ ~
:
6 Case 5279 ~ which is in turn received by the data acquisition system !i ' 95. All of this information received can be provided to an operator through the use of a CRT 99 linked to the data ac~uisition system 95.
Because there are special needs involved in the remediation of mixed waste the following can be , incorporated into the present invention~
d First, the circulating fluidized bed 10 can be fired with a clean auxiliary fuel such as gas or oil in the burner 14.
Second, the mixed waste can be fed above the bed so as to allow the greatest flexibility in accepting a wide range of wastes and sizes, thereby, minimizing the preprocessing of the waste for size reduction.
; 15 Third, in this system 10 the secondary cyclone ^ separator 30 can be replaced by a variable efficiency cyclone separator. A variable efficiency cyclone will allow close control of the radioactive waste that is sent to the tertiary separator 40. As the concentration J 20 of radioactive material in the cyclone recycle stream 32 increases, the efficiency of the cyclone would be - "spoiled" allowing more of the waste to pass to the tertiary separator 40. This would enable the operator . to minimize the total amount of low level radioactive 25 waste that would have to be sent to a nuclear waste storage vault. The balance of the waste, which would be "clean", would be removed from the bed drain 58 and would be sent back to an appropriate disposal site. The variable efficiency cyclones can operate in a range of "`~ 9 ,~J 1 ~ ~ :
7 Case 5279 size separation conducive to the isolation of radioactive waste.
Fourth, tertiary separation can be performed with a high efficiency particulate filter instead of a conventional baghouse or electrostatic precipitator.
The high efficiency particulate filter can ensure that no radioactive waste escapes from the system in the flue gas stream.
Fifth, the system 10 can be portable by loading it onto a flat bed truck for set up at the site.
The circulating fluidized bed combustor system 10 has other advantages in addition to those mentioned above. The strong mixing in the furnace 54 and high solids circulation rate from the L-valve 22 and cyclone recycle lines 32 promote attrition of the mixed waste.
This effect promotes the complete burnout of the combustible organic constituents of the waste as well as break up of the agglomerates containing trace amounts of radioactive material. The attrition of the agglomerates further enhances the effectiveness of the variable efficiency cyclone 30 to separate the trace radioactive material from "clean" solids.
With air staging it is possible to operate the ~- lower furnace 54b at a temperature below the agglomerating temperature of ~he waste material, and an upper furnace 54a at a temperature (1700-1800 F) suitable for the complete destruction of organic constituents such as dioxins, PCBs, or furans. The height of the circulating fluidized bed 10 provides the 3Q necessary residence time for complete destruction of the . ~
~ , J ,~ ~ ~
8 Case 5279 ~' organics. The degree of staging and the optimum gas J~ time/temperature history can be determined for the present invention. The air staging also minimizes the production of nitrogen oxide emissions.
The process described above is based on a - circulating fluidized bed incinerator operating at near atmospheric pressure, but could also be implemented in a pressurized fluidized bed with some variations. A
pressurized fluidized bed is a more compact system since it operates at 10 to 15 times atmospheric pressure.
The circulating fluidized bed or the - pressurized fluidized bed could be fired with oxygen -~ enrichment to even further reduce the furnace and collection equipment size.
Ammonia injection could be used to further reduce nitrogen oxide emissions.
~ Limestone addition to the furnace or a scrubber - downstream of the furnace could be used to control SO2 emissions.
While a specific embodiment of the invention has been shown and described in detail to illustrate the application of the principles of the invention, it will be understood that the invention may be embodied otherwise without departing from such principles.
54. A wind box burner 12 preheats the air from the air~
lines 16.
~ater is provided in furnace cooling tubes 56 arranged through the furnace 54 to allow adjustment of bed temperatures.
Upon burning of materials within the bed 50, combustion gases emanate from the bed 50 and pass through the furnace 54 to a primary separator 20. The ~, primary separator 20 is located above the bed 50 and at the top of the furnace 54. The primary separator 20 is constructed of U-beams which are stainless steel channels installed in a labyrinth arrangement. The primary separator 20 removes large entrained bed material such as sand, lime, flyash or unburned fuel particles from the flue gas.
~` After passing through the primary separator 20, the combustion gas is then channeled through a convection pass cooling bundle 26 to a secondary cyclone .
separator 30. The secondary cyclone separator 30 separates fines from the flue gas.
After passing through the secondary cyclone separator 30 the flue gas is channeled through a second pass 36 to a tertiary separator 40 for tertiary separation~ The tertiary separator 40 may consist of a high efficiency particulate filter, such as a Hepa~
filter. Any solids collected at the tertiary separator 40 are channelled to a collection container 44.
~02~
~ 5 Case 5279 ,.~
Solids separated from the gas by the secondary cyclone separator 30 are recycled back into the bed 50 by a transport system 32 which recycles the solids to a recycle point 80 located near the furnace 54. The recycle point 80 then channels the recycled solids from the secondary cyclone separator 30 back into the bed 50.
Larger size solid particles captured by the primary separator 20 are channeled through a stand pipe 24 which runs parallel with the furnace 54 to a L-valve 22. The L-valve 22 transports these recycled solids directly into the bed 50. Additionally, solids can be discharged into a secondary collection container 34 located at the secondary cyclone separator 30.
Solids can be drained from the circulating fluidized bed combustor 10 by a bed drain 58 which directly drains solids from the bed 50, from the secondary cyclone 30 at the collection container 34 or ~ from the tertiary separator 40.
- Fig. 2 shows a computerized data acquisition 2Q system 90 for the continuous monitoring of operating conditions of the circulating fluidized bed combustor dat~ CrC ~ 5;h'orJ '~v,St~
10. The ~e~ 90 'periodically scans system~ ~ P~
temperatures, air and gas flow rates, and system static~
and differential pressures.
The flue gas exiting the tertiary collector 40 is continuously monitored for 2~ C unburned hydrocarbons and other gas constituents necessary to control the process. Thermocouple inputs 97 located at the circulating fluidized bed combustor 10 provide temperature information to the thermocouple junction 98 fJ.JL~?J ~ ~
:
6 Case 5279 ~ which is in turn received by the data acquisition system !i ' 95. All of this information received can be provided to an operator through the use of a CRT 99 linked to the data ac~uisition system 95.
Because there are special needs involved in the remediation of mixed waste the following can be , incorporated into the present invention~
d First, the circulating fluidized bed 10 can be fired with a clean auxiliary fuel such as gas or oil in the burner 14.
Second, the mixed waste can be fed above the bed so as to allow the greatest flexibility in accepting a wide range of wastes and sizes, thereby, minimizing the preprocessing of the waste for size reduction.
; 15 Third, in this system 10 the secondary cyclone ^ separator 30 can be replaced by a variable efficiency cyclone separator. A variable efficiency cyclone will allow close control of the radioactive waste that is sent to the tertiary separator 40. As the concentration J 20 of radioactive material in the cyclone recycle stream 32 increases, the efficiency of the cyclone would be - "spoiled" allowing more of the waste to pass to the tertiary separator 40. This would enable the operator . to minimize the total amount of low level radioactive 25 waste that would have to be sent to a nuclear waste storage vault. The balance of the waste, which would be "clean", would be removed from the bed drain 58 and would be sent back to an appropriate disposal site. The variable efficiency cyclones can operate in a range of "`~ 9 ,~J 1 ~ ~ :
7 Case 5279 size separation conducive to the isolation of radioactive waste.
Fourth, tertiary separation can be performed with a high efficiency particulate filter instead of a conventional baghouse or electrostatic precipitator.
The high efficiency particulate filter can ensure that no radioactive waste escapes from the system in the flue gas stream.
Fifth, the system 10 can be portable by loading it onto a flat bed truck for set up at the site.
The circulating fluidized bed combustor system 10 has other advantages in addition to those mentioned above. The strong mixing in the furnace 54 and high solids circulation rate from the L-valve 22 and cyclone recycle lines 32 promote attrition of the mixed waste.
This effect promotes the complete burnout of the combustible organic constituents of the waste as well as break up of the agglomerates containing trace amounts of radioactive material. The attrition of the agglomerates further enhances the effectiveness of the variable efficiency cyclone 30 to separate the trace radioactive material from "clean" solids.
With air staging it is possible to operate the ~- lower furnace 54b at a temperature below the agglomerating temperature of ~he waste material, and an upper furnace 54a at a temperature (1700-1800 F) suitable for the complete destruction of organic constituents such as dioxins, PCBs, or furans. The height of the circulating fluidized bed 10 provides the 3Q necessary residence time for complete destruction of the . ~
~ , J ,~ ~ ~
8 Case 5279 ~' organics. The degree of staging and the optimum gas J~ time/temperature history can be determined for the present invention. The air staging also minimizes the production of nitrogen oxide emissions.
The process described above is based on a - circulating fluidized bed incinerator operating at near atmospheric pressure, but could also be implemented in a pressurized fluidized bed with some variations. A
pressurized fluidized bed is a more compact system since it operates at 10 to 15 times atmospheric pressure.
The circulating fluidized bed or the - pressurized fluidized bed could be fired with oxygen -~ enrichment to even further reduce the furnace and collection equipment size.
Ammonia injection could be used to further reduce nitrogen oxide emissions.
~ Limestone addition to the furnace or a scrubber - downstream of the furnace could be used to control SO2 emissions.
While a specific embodiment of the invention has been shown and described in detail to illustrate the application of the principles of the invention, it will be understood that the invention may be embodied otherwise without departing from such principles.
Claims (11)
1. A method for the remediation of low level radioactive mixed waste in a fluidized bed incinerator, the method comprising;
feeding the waste into the incinerator for combusting into a flue gas;
channeling the flue gas through a primary separator for entraining and collecting large particles from the flue gas;
channeling the flue gas from the primary separator to a secondary separator for entraining and collecting small particles from the flue gas;
channeling the flue gas from the secondary separator to a tertiary separator for entraining and collecting fine particles from the flue gas;
recycling the particles collected at the primary separator back into the incinerator for further combusting;
recycling the particle collected at the secondary separator back into the incinerator for further combusting; and removing the fine particles collected at the tertiary separator for treatment as low-level radioactive waste.
feeding the waste into the incinerator for combusting into a flue gas;
channeling the flue gas through a primary separator for entraining and collecting large particles from the flue gas;
channeling the flue gas from the primary separator to a secondary separator for entraining and collecting small particles from the flue gas;
channeling the flue gas from the secondary separator to a tertiary separator for entraining and collecting fine particles from the flue gas;
recycling the particles collected at the primary separator back into the incinerator for further combusting;
recycling the particle collected at the secondary separator back into the incinerator for further combusting; and removing the fine particles collected at the tertiary separator for treatment as low-level radioactive waste.
2. The method according to Claim 1, wherein a clean fuel is used to fire the incinerator.
3. The method according to Claim 1, wherein an operator monitors the amount of radioactive particles recycled back into the incinerator.
4. A fluidized bed incinerator system for the remediation of low-level radioactive mixed waste, the system comprising:
a fluidized bed for combusting waste into a flue gas;
means for feeding waste to the fluidized bed;
a flue gas pathway for channeling the flue gas away from the fluidized bed;
a first separator located in the flue gas pathway for collecting large particles from the flue gas;
a second separator located in the flue gas pathway after the first separator for collecting smaller particles from the flue gas;
a third separator located in the flue gas pathway after the second separator for collecting fine particles from the flue gas;
means for recycling particles collected at the first and second separators back into the fluidized bed for further combusting; and means for removal of the fine particles collected at the third separator for treatment as radioactive waste.
a fluidized bed for combusting waste into a flue gas;
means for feeding waste to the fluidized bed;
a flue gas pathway for channeling the flue gas away from the fluidized bed;
a first separator located in the flue gas pathway for collecting large particles from the flue gas;
a second separator located in the flue gas pathway after the first separator for collecting smaller particles from the flue gas;
a third separator located in the flue gas pathway after the second separator for collecting fine particles from the flue gas;
means for recycling particles collected at the first and second separators back into the fluidized bed for further combusting; and means for removal of the fine particles collected at the third separator for treatment as radioactive waste.
5. The system according to Claim 4, wherein the fuel is supplied to the system at a location in the furnace above the dense phase portion of the bed.
6. The system according to Claim 4, wherein the waste is supplied to the system at a location in the furnace above the dense phase portion of the bed.
7. The system according to Claim 5, wherein the fuel is clean.
8. The system according to Claim 4, wherein the second separator is a variable efficiency separator for controlling the amount of radioactive waste sent to the third separator.
9. The system according to Claim 4, wherein the third separator is a high efficiency particulate filter.
10. The system according to Claim 4, wherein the system is portable.
11. The system according to Claim 4, wherein the means for recycling particles collected at the first and second separators back into the fluidized bed comprises an L-valve for recycling particles collected by the first separator and a transport system for recycling particles collected by the second separator.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US970,726 | 1992-11-03 | ||
| US07/970,726 US5353718A (en) | 1992-11-03 | 1992-11-03 | Remediation of low level radioactive mixed waste in a fluidized bed incinerator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2102160A1 true CA2102160A1 (en) | 1994-05-04 |
Family
ID=25517409
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002102160A Abandoned CA2102160A1 (en) | 1992-11-03 | 1993-11-01 | Remediation of low level radioactive mixed waste in a fluidized bed incinerator |
Country Status (2)
| Country | Link |
|---|---|
| US (1) | US5353718A (en) |
| CA (1) | CA2102160A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110772919A (en) * | 2019-11-25 | 2020-02-11 | 成都天保节能环保工程有限公司 | Radioactive organic waste steam reforming gas purification system and technological method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6119607A (en) * | 1997-05-09 | 2000-09-19 | Corporation De L'ecole Polytechnique | Granular bed process for thermally treating solid waste in a flame |
| EP1079915B1 (en) * | 1999-03-12 | 2004-10-13 | EISENMANN MASCHINENBAU KG (Komplementär: EISENMANN-Stiftung) | Method for disposing of hazardous and high-energy materials and device for carrying out said method |
| JP2014152973A (en) * | 2013-02-07 | 2014-08-25 | Ube Machinery Corporation Ltd | Mobile incineration facility |
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| FR2545916B1 (en) * | 1983-05-10 | 1985-07-19 | Fives Cail Babcock | PLANT FOR THE HEAT TREATMENT OF POWDER MINERALS |
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| DE3604318C2 (en) * | 1986-02-12 | 1994-01-13 | Metallgesellschaft Ag | Process for burning cow dung |
| DE3724563A1 (en) * | 1987-07-24 | 1989-02-02 | Kernforschungsanlage Juelich | METHOD FOR THERMALLY TREATING WASTE AND APPARATUS FOR CARRYING OUT THIS METHOD |
| US4991521A (en) * | 1988-04-12 | 1991-02-12 | Mobil Oil Corporation | Fluidized bed combustion process and apparatus |
| US5069170A (en) * | 1990-03-01 | 1991-12-03 | Foster Wheeler Energy Corporation | Fluidized bed combustion system and method having an integral recycle heat exchanger with inlet and outlet chambers |
| US5206176A (en) * | 1990-10-02 | 1993-04-27 | Massachusetts Institute Of Technology | Detection and control of aromatic compounds in combustion effluent |
-
1992
- 1992-11-03 US US07/970,726 patent/US5353718A/en not_active Expired - Fee Related
-
1993
- 1993-11-01 CA CA002102160A patent/CA2102160A1/en not_active Abandoned
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110772919A (en) * | 2019-11-25 | 2020-02-11 | 成都天保节能环保工程有限公司 | Radioactive organic waste steam reforming gas purification system and technological method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| US5353718A (en) | 1994-10-11 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| EEER | Examination request | ||
| FZDE | Discontinued |